FOAM BLOWING AGENT COMPOSITION AND PROCESS FOR PRODUCING FOAMS

Description

FIELD OF THE INVENTION

[0001] This invention relates to a blowing agent composition and the method used to prepare a polymeric styrenic foam.

BACKGROUND OF THE INVENTION

[0002] Thermoplastic foams made from styrenic polymers such as polystyrene have found extensive use, particularly in food packaging and food service applications. The key to a successful polystyrene foam for food applications is to use a blowing agent compcsition during the formation of the foam that diffuses out of the cells and is substantially replaced by air before the foam comes into contact with any food to be packaged or served.

[0003] Generally, polystyrene foams are manufactured by mixing a volatile blowing agent with the styrenic resin under a controlled temperature and pressure sufficient to plasticize the resin and to maintain the resin blowing agent composition in an unfoamed state. Thereafter the molten mixture of resin and blowing agent and sometimes a nucleator is extruded through an annular die into a zone of lower temperature and pressure. If extrusion conditions are optimum, a tube of rigid, closed cell foam will be produced.

[0004] This tube is usually stretched over a mandrel of larger diameter. Stretching not only yields a larger tube of foam but also "orients" and strengthens or toughens the foam.

[0005] The tube is then slit and opened up to form at least one flat sheet. The sheet (or sheets) is usually stored in large rolls and aged for at least 24 hours. The aging process is required to obtain "post expansion" during the subsequent thermoforming operation.

[0006] "Post expansion" refers to the swelling of the foam as it is heated in the thermoformer oven. This expansion is the result of the different permeation rates of air and the blowing agent through the foam cell walls. As the foam emerges from the die during the extrusion step, the cells containing the blowing agent tend to expand until the pressure within the cells equals the atmospheric pressure outside the cells. During the aging period, air permeates rapidly into the cells; but the blowing agent (having a larger size molecule than air) permeates out relatively slowly. The result is an increase of cell gas pressure during aging. The gas pressure increases from 1 atmosphere to about 2 atmospheres. When the foam is subsequently heated and softened, this increased gas pressure causes the foamed product to expand further, i.e., "post expand".

[0007] Dichlorodifluoromethane (CFC-12) historically has been the blowing agent of choice in producing polystyrene foam. With the planned phase-out of CFC-12 as a foam blowing agent because of its measurable undesirable Ozone Depletion Potential (ODP) and the unacceptability of chlorodifluoromethane (HCFC-22) as a long term alternative blowing agent in food packaging/food service use, there is a critical need for an acceptable alternative blowing agent. Hydrocarbon blowing agents, although having zero ODPs, are less desirable for use in food containers since they are classified as photochemically reductive volatile organic compounds (VCCs) and their use is regulated by law.

[0008] EP-A-0427533 discloses insulating foams of an alkenyl aromatic compound such as styrene which have an average cell size of 0.01 to 0.3 millimetres. The cells are non-interconnecting and contain at least 7C percent by weight of 1,1,1-trifluoroethane or 1,1,1,2-tetrafluoroethane.

[0009] US-A-4528300 describes a process for preparing olefin foams, such as polyethylene, using as a blowing agent a mixture of 1-chloro-1,1-difluoroethane or of 1,1-difluoroethane with an aliphatic hydrocarbon, the aliphatic hydrocarbons or halogenated hydrocarbons having specified boiling points and vapour pressures. The resulting foams are claimed to have reduced shrinkage.

[0010] EP-A-0385349 is concerned with the production of alkenyl aromatic foams, such as polystyrene, having small average cell sizes, improved compressive strengths and higher cell volumes. Blowing agents employed are one or more of l-chloro-1,1-difluoro-ethane, 1,1,1,2-tetrafluoroethane and 2-chloro-1,1,1,2-tetrafluoroethane.

[0011] EP-A-0425886 describes a process for manufacturing foams by expanding thermoplastic resin beads using high frequency energy. A very large number of blowing agents are stated to be usable in the process, including hydrocarbons, fluorocarbons and other halogenated hydrocarbons, and difluoroethane is mentioned. Likewise, an extensive list of thermoplastic resins is mentioned including styrene polymers.

[0012] It is an object of this invention to provide a blowing agent for thermoplastic styrenic polymers that displays a zero ODP and is not substantially photochemically reactive, that can be processed in a manner such that it diffuses substantially completely from the ultimate foamed product, and that. even if a slight amount remained in the product, it would be so low as not to be considered a component of any food served or contained within the foamed product.

[0013] It is a further object to provide an operable process for utilizing the aforementioned blowing agent in the manufacture of a polymeric styrene foam product, particularly in the manufacture of a thermoplastic composition such as polyethylene or polystyrene.

[0014] In accordance with the present invention there is provided a extruded closed-cell polymer foam wherein the cells are free from fluorocarbon blowing agent, said foam having been prepared from a foam-forming composition comprising a styrene resin and up to 20 weight percent, based on the total weight of the composition, of 1,1-difluoroethane, said foam having a thickness from 1 to 5.08 mm (0.04 to 0.2 inches), the foam having been stretched after extrusion, aged in air for a period of at least 24 hours and subjected to heating to cause post expansion of the foam and replacement of the 1,1-difluoroethane with air.

[0015] Of course. nitrogen, carbon dioxide, other inert gases, hydrocarbons and chemical blowing agents can be used in conjunction with the polyfluorocarbon blowing agent.

[0016] The ultimate polymeric foam product of this invention is characterized in that the cells of the foam are free from polyfluorocarbon blowing agent.

[0017] The cells of the foam are substantially completely filled with air, making the foam produced suitable for food contact applications.

[0018] The preference for HFC-152a in polystyrene packaging foams is based on the following four characteristics:-

1. Low environmental impact; zero ODP, very low HGWP, (haiocarbon global warming potential) or "greenhouse effect", and has been added to the list of organic compounds which are negligibly reactive and thus may be exempt from regulation under state implementation plans (SIP's) to attain the national ambient air quality standards (NAAQ's) for ozone;

2. Low molecular weight: less amount of HFC-152a is required to achieve similar density as existing foams;

3. Low cost per pound; and

4. Rapid diffusion from foams; imperative for food service and food packaging applications.

[0019] The invention also provides a process for producing a closed-cell polymer foam whose cells are completely filled with air, said process comprising introducing 1,1-difluoroethane as a blowing agent into a molten styrenic resin in an extruder, extruding a tubular foamed product therefrom, stretching the foamed product, ageing the stretched foam in air for at least 24 hours to allow sufficient time for air to permeate through the cell walls of the foam to cause an increase in pressure therein, and heating the aged foam to cause post expansion.

[0020] The packaging foams should be produced using no added water, preferably in the absence of any water. It has been found that the use of water in polystyrene foam production causes large unacceptable voids (steam pockets) in the resulting foam product. It is believed that this is due to the poor solubility of water in these polymers. However, small amounts of water (1-4 wt.%) may be used if an appropriate solubilizing or dispersing agent (alcohol, glycol, surfactants etc.) is also used.

[0021] In the preparation of foams in accordance with the method of the invention, it is often desirable to add a nucleating agent to the styrenic resin. These nucleating agents serve primarily to increase cell count and reduce the cell size in the foam and are used in an amount of about 0.1 part by weight to about four parts by weight per one hundred parts resin. For example, talc, sodium bicarbonate/citric acid, gaseous CO₂, calcium silicate and the like are suitable nucleating agents for reducing cell size. Talc is a preferred nucleating agent component in the practice of the method of the invention. Various other additives, for example, fire retardant additives, color concentrates, stabilizers, anti-oxidants, lubricants, etc. may also be used depending on the end use of the styrenic foam.

[0022] In accordance with the method of the invention, a styrenic foam is produced from a "styrenic resin", which means a solid polymer of one or more polymerizable alkenyl aromatic compounds or a compatible mixture of such polymers. Such an alkenyl aromatic compound has the general formula:

wherein R₁ represents an aromatic hydrocarbon radical of the benzene or substituted benzene series, and R₂ is either hydrogen or the methyl radical. Examples of such alkenyl aromatic compounds are styrene, alpha-methyl styrene, ortho-methyl styrene, meta-methyl styrene, paramethyl styrene. The solid copolymers of one or more of such alkenyl aromatic compounds with amounts of other polymerizable compounds such as methylmethacrylate, acrylonitrile, maleic anhydride and acrylic acid are also operable in this invention. The preferred styrenic resin is the homopolymer, polystyrene, which is readily available from various sources.

[0023] In the method of the invention, the styrenic resin is mixed with a blowing agent composition and the resulting mixture is then foamed. Preferably, the foaming is carried out with the use of an extruder, wherein the styrenic polymer is heated to about 204-232°C (400°-450°F), to produce a molten polymer and the blowing agent is then introduced into the extruder where it is mixed with the molten polymer under pressures such that the resulting plasticized extrusion mass does not foam, but its viscosity decreases. The extrusion mass is then cooled. Cooling increases the viscosity and the melt strength of the mass prior to extrusion. The mass is then extruded through a die of any desirable shape of a controlled temperature, usually about 149°C (300°F), the reduced pressure outside the extruder permitting the extrusion mass to foam.

[0024] The temperature and pressure conditions under which the styrenic resin and blowing agent mixture will not foam will depend upon the particular styrenic resin used and generally, will be at a temperature between about 116°C (240°F), and about 227°C (440°F), and a pressure above about 4136 kPa (600 psig).

[0025] The conditions of temperature and pressure under which the extrusion mass will foam, again will depend upon the precise styrenic resin used and generally will be at a similar temperature of about 116°C and 227°C (240°F and 440°F), but at a lower pressure. However, the more precise the temperature is controlled throughout the extrusion process, the more uniform the resulting foam.

[0026] The melt plasticization is controlled by the choice of the particular polyfluorocarbon blowing agent composition, the amount of and type of nucleating agent or other additive(s) present, the particular styrenic resin or mixture being used and the Tg or Tg's of the resin(s) and the temperature, pressure in the extruder and the extrusion rate. The shaping means used can also affect the orientation of the polymer.

[0027] In practicing the method of the invention, the blowing agent may be added to the styrenic resin in any desirable manner and, preferably, by injection of a stream of the blowing agent composition directly into the molten styrenic resin in the extruder. The blowing agent should be mixed thoroughly with the styrenic resin before the blowing agent and styrenic resin mass is extruded from the die. This is necessary to produce a foam having uniform density and cellular structure.

[0028] The extrusion mass comprising the molten resin and the blowing agent composition is extruded into an expansion zone within which foam formation and expansion takes place. Any suitable extrusion equipment capable of processing polystyrenic compositions can be used for the extrusion. Single or multiple-screw extruders can be used. Softening the polymer and mixing with the blowing agent take place during working of the polymer between flights of the screw or screws, which also serve to convey the extrusion mass to the extruder die. Screw speed and extruder barrel temperature should be such as to achieve adequate mixing and softening but not so high as to degrade the composition being processed.

[0029] The foams can be used in the form prepared, cut into other shapes, further shaped by application of heat and pressure or otherwise machined or formed into shaped articles of desired size and shape.

[0030] For the foams to have utility in the food service and food packaging application, the tubular foamed product from the initial foaming zone or stage is fed over a mandrel of larger diameter to be stretched anywhere from 1.2 to about 5 times its original diameter.

[0031] After stretching, the tube is slit and opened to form a flat sheet. The flat sheet is stored on a roll. The rolls are aged in air over a period of at least about 24 hours but usually less than 2 weeks, i.e. sufficient time for air to permeate through the cell walls of the foam, but because of storage in rolls of foamed sheet, insufficient time for any substantial amount of the polyfluorocarbon blowing agent to diffuse out. The result is a substantial increase in gas pressure within the cells. When the foamed product is heated and softened in the final step of the process, the increased gas pressure causes the foamed product to expand further, i.e. post expand. The polyfluorocarbon then diffuses substantially completely from the final foamed product and is replaced by air.

[0032] The following Examples are intended to illustrate the present invention.

EXAMPLE 1

[0033] In this example, polystyrene foam sheet was prepared using HFC-152a as the blowing agent; and was compared to a similar product prepared using HCFC-22 as the "control" blowing agent.

[0034] It was concluded that HFC-152a was a very efficient blowing agent. About 25 percent less of HFC-152a than the control was required to achieve a similar density polystyrene foam.

[0035] The post-expansion characteristics of foam sheet produced with HFC-152a were superior to foam produced with the control.

[0036] The polystyrene foam sheet using HFC-152a thermoformed into excellent quality egg cartons and hamburger containers.

[0037] The comparative test (HFC-152a vs. the control) was conducted using a conventional tandem extrusion system. Foam was extruded through an annular die, stretched over a mandrel about 4 times the die's diameter, and slit to produce a single sheet.

[0038] The extrusion system was started using the control blowing agent. After about 25 minutes, HFC-152a was introduced from cylinders pressurized with nitrogen.

[0039] In the following table, Table 1, the data using HFC-152a and the control as blowing agents are compared:

Table 1

	HFC-152a	Control
Extrusion rate g/s (lbs/hr)	88.2 (700)	88.2 (700)
Blowing, agent injection rate g/s (lbs/hr)	4.03 (32)	5.04 (40)
Die pressure MPa (psig)	7.534 (1100)	7.998 (1160)
Melt temperature °C (°F)	148.9 (300)	146.1 (295)
Foam density kg/m3 (pcf)	79.49 (4.9)	80.09 (5)
Sheet gauge mm (mils)	2.896 (114)	2.896 (114)

[0040] Foam sheet produced in this test using HFC-152a was successfully thermoformed after 7, 14, 21 and 28 days' aging, whereas the control failed to produce acceptable product after 21 days.

EXAMPLE 2

[0041] In the following table, Table 2, the important properties of HFC-152a are compared to CFC-12 and HCFC-22:

Table 2

	CFC-12	HCFC-22	152a
Molecular Weight	120.9	86.5	66
Boiling point (°C)	-29.8	-40.8	-25.0
ODP	1.0	0.05	0
HGWP	3.1	0.34	0.03

[0042] The ozone depletion potential (ODP) was calculated using the method described in "The Relative Efficiency of a Number of Halocarbon for Destroying Straospheric Ozone: D. J. Wuebles, Lawrence Livermore Laboratory report UCID-18924, (January 1981) and "Chlorocarbon Emission Scenarios: Potential Impact on Stratospheric Ozone" D. J. Wuebles, Journal Geophysics Research, 88, 1433-1443 (1983).

[0043] Basically, the ODP is the ratio of the calculated ozone depletion in the stratosphere resulting from the emission of a partcular agent compared to the ODP resulting from the same rate of emission of CFCl₃, (CFC-11) which is set at 1.0. Ozone depletion is believed to be due to the migration of compounds containing chlorine or bromine through the troposphere into the stratosphere where these compounds are photolyzed by UV-radiation into chlorine or bromine atoms. These atoms will destroy the ozone (O₃) molecules in a cyclical reaction where molecular oxygen (O₂) and [ClO] or [BrO] radicals are formed, those radicals reacting with oxygen atoms formed by UV-radiation of O₂ to reform chlorine or bromine atoms and oxygen molecules, and the reformed chlorine or bromine atoms then destroying additional ozone, etc., until the radicals are finally scavenged from the stratosphere. It is estimated that one chlorine atom will destroy 10,000 ozone molecules.

[0044] The ozone depletion potential is also discussed in "Ultraviolet Absorption Cross-Sections of Several Brominated Methanes and Ethanes" L. T. Molina, M. J. Molina and F. S. Rowland" J. Phys. Chem. 86, 2672-2676 (1982); in Bivens et al. U.S. Patent 4,810,403; and in "Scientific Assessment of Stratospheric Ozone: 1989" U. N. Environment Programme (21 August 1989).

[0045] The global warming potentials (GWP) are determined using the method described in 'Scientific Assessment of Stratospheric Ozone: 1989" sponsored by the U. N. Environment Programme.

[0046] The GWP, also known as the "greenhouse effect" is a phenonmenon that occurs in the troposphere. It is calculated using a model that incorporates parameters based on the agent's atmospheric lifetime and its infra-red cross-section or its infra-red absorption strength per mole as measured with an infra-red spectrophotometer.

[0047] The general definition is:

divided by the same ratio of parameters for CFCl₃.

EXAMPLE 3

[0048] The permeation and diffusion properties of HFC-152a relative to polystyrene were determined in this example.

[0049] In Figure 1, the permeation coefficient of HFC-152a is compared to the coefficients for CFC-12, HCFC-142b, HCFC-22, and nitrogen at temperatures of 20°C to 160°C.

[0050] In Figure 2, the permeation rate for HFC-152a through polystyrene film is presented for various pressure drops across the film at temperatures of 20°C to 100°C.

[0051] In Figure 3, the diffusion coefficient of HFC-152a into polystyrene is presented at various temperatures from 20°C to 160°C.

[0052] The permeation tests were conducted by a modification of ASTM D1434-82, "Standard Method for Determining Gas Permeability Characteristics of Plastic Film and Sheeting". This modified procedure is described in the Master of Chemical Engineering Thesis, P. S. Mukherjee, Widener University, Chester, PA, February 1988, entitled "A Study of the Diffusion and Permeation Charac teristics of Fluorocarbons Through Polymer Films":

(1) Using a Barber-Coleman press, 30 g samples polystyrene (as pellets) were pressed into 0.1524 m x 0.1524 m (6" x 6") sheets of film with 0.381 nm-0.503 nm (15-20 mil) thickness. The pressing was done at 400°F and at a pressure of about 241.32 MPa (35,000 psig) (maintained for 5 minutes).

(2) Discs 0.381 nm-0.503 nm (15-20 mil thickness) were cut from 0.1524 m x 0.1524 m (6" x 6") sheets of film. Five discs of 0.1524m-0.1524m (47 mm diameter) were made from each sheet. The discs were cut or stamped at ambient temperature using a die punch made of A-2 type steel (hardened).

(3) All tests were run at a 137.9 kPa (20 psia) pressure differential between the high pressure side and the low pressure side of the permeation cell.

(4) Permeation tests were run at 20° to 160°C, with tests for each polystrene/gas combination being run at at least 5 temperatures.
Data for other temperatures were calculated from the equation:

wherein P is permeation coefficient, T is °K (C + 273.2) and A and B are constants determined from the permeation coefficients calculated from the following equation:

(5) The permeation rates are based on a 1 cm² by 1 cm thick film with a 6.895 kPa (1.0 psia) pressure drop across the film.
To obtain the permeation coefficient (P), the standard permeation equation is used. It is based on Fick's law of diffusion and Henry's law of solubility.

   * at 0°C and 1 atmosphere of pressure.

[0053] The diffusion coefficient for each experimental temperature was determined by extrapolating the straight-line plot of low-side pressure versus time, obtained in the permeation study to the time axis. This time, referred to as lag time in literature, is used to obtain the diffusion coefficient by means of this equation:

   where

D = diffusion coefficient, cm²/sec.

x = plastic film thickness, cm

t = lag time, seconds

[0054] Based on the data shown in the figures, it is apparent that HFC-152a exhibits permeation characteristics similar to HCFC-22 with polystyrene. The permeation coefficients for HFC-152a are nearly identical to HCFC-22 but the diffusion coefficients differ. The diffusion coefficient for HFC-152a changes much less over the temperature range 20°-100°C than the coefficient for HCFC-22. This is an indication of the solubility difference between the two compounds relative to polystyrene.

[0055] The foregoing indicates that HFC-152a is a good candidate for foaming polystyrene sheet for food service and food packaging containers. This blowing agent readily permeates from the foam but still provides effective post expansion (better than HCFC-22), because the remaining blowing agent is in the cells, not the polymer.

EXAMPLES 4 AND 5

[0056] In these examples, two different foam sheets were produced using a 0.1143m/0.1514m (4.5 inch/6 inch) tandem extrusion line; Example 4, 155/m² (10 g/100 square inches); Example 5, 17 g/100 square inches.

[0057] The manufacturing and test data are presented in Table 4.

Table 4

	Example 4	Example 5
	155/m2 (10 g/100 sg.in.)	264/m2 (17 g/100 sg.in.)
Formulation
Polystyrene (%)	95.3	96.5
HFC-152a (%)	4.4	3.1
Talc (%)	0.4	0.4

Foam Product
Thickness mm (mil)	2.159 (85)	2.159 (85)
Density kg/m3 (pcf)	57.67 (3.6)	94.51 (5.9)
Cell size mm (mil)	0.099 (3.9)	0.203 (8.0)

Foam Thickness After Post-Expansion mm (mils)
after 1 day	5.004 (197)	5.359 (211)
2 days	4.775 (188)	4.293 (169)
3 days	4.750 (187)	4.801 (189)
4 days	6.096 (240)	4.420 (174)
6 days	6.198 (244)	5.182 (204)
7 days	6.274 (247)	5.944 (234)
10 days	5.690 (224)	5.030 (198)
14 days	5.436 (214)	5.867 (231)
21 days	6.350 (250)	5.436 (214)
24 days	6.731 (265)	5.461 (215)

Claims

1. An extruded closed-cell polymer foam wherein the cells are free from fluorocarbon blowing agent. said foam having been prepared from a foam-forming composition comprising a styrene resin and up to 20 weight percent, based on the total weight of the composition. of 1,1-difluoroethane, said foam having a thickness from 1 to 5.08 mm (0.04 to 0.2 inches). the foam having been stretched after extrusion, aged in air for a period of at least 24 hours and subjected to heating to cause post expansion of the foam and replacement of the 1,1-difluoroethane with air.

2. A polymer foam as claimed in claim 1 wherein the foam is stretched after extrusion by an amount of from 1.2 to 5 times its original diameter.

3. A process for producing a closed-cell polymer foam as claimed in claim 1 whose cells are completely filled with air. said process comprising introducing 1,1-difluoroethane as a blowing agent into a molten styrenic resin in an extruder, extruding a tubular foamed product therefrom, stretching the foamed product, ageing the stretched foam in air for at least 24 hours to allow sufficient time for air to permeate through the cell walls of the foam to cause an increase in pressure therein, and heating the aged foam to cause post expansion.

4. A process as claimed in claim 3 wherein the foamed product is stretched by an amount of from 1,2 to 5 times its original diameter after the extrusion step.

5. A process as claimed in claim 3 or 4 wherein said styrenic resin and the blowing agent are subjected to a temperature and pressure in the extruder such that the resin does not foam and the viscosity of the molten resin decreases, thereafter the temperature is reduced to increase the viscosity of the molten resin and the molten resin is extruded into a zone at a temperature and pressure sufficient to permit foaming.

6. A process as claimed in claim 5 wherein the temperature and pressure at which the mixture does not foam is from about 116°C (240°F) to about 227°C (440°F), and a pressure above about 4136 kPa (600 psig).

7. A process as claimed in any one of claims 3 to 6 which is carried out in the substantial absence of water.

8. A process as claimed in any one of claims 3 to 7 further comprising the step of adding a nucleating agent to the polystyrene resin.

9. A process as claimed in claim 8 wherein the nucleating agent is talc. sodium bicarbonate/citric acid, gaseous CO₂ or calcium silicate.

Ansprüche

1. Extrudierter geschlossenzelliger Polymerschaum, in welchem die Zellen frei von einem Fluorkohlenstoff-Treibmittel sind, wobei der Schaum aus einer schaumbildenden Zusammensetzung hergestellt worden ist, welche ein Styrolharz und bezogen auf das Gesamtgewicht der Zusammensetzung bis zu 20 Gew.-% an 1,1-Difluorethan umfaßt, der Schaum eine Dicke von 1 bis 5,08 mm (0,04 bis 0,2 inch) besitzt, der Schaum nach dem Extrudieren gestreckt worden ist, an Luft während eines Zeitraums von mindestens 24 Stunden gealtert wurde und einer Erwärmung unterzogen wurde, um eine Nachexpansion des Schaumes und einen Austausch des 1,1-Difluorethans gegen Luft zu bewirken.

2. Polymerschaum gemäß Anspruch 1, wobei der Schaum nach dem Extrudieren um das 1,2- bis 5-fache seines ursprünglichen Durchmessers gestreckt wird.

3. Verfahren zur Herstellung eines wie in Anspruch 1 beanspruchten geschlossenzelligen Polymerschaums, dessen Zellen vollständig mit Luft gefüllt sind , wobei das Verfahren das Einbringen von 1,1-Difluorethan als ein Treibmittel in ein geschmolzenes Styrolharz in einem Extruder, das daraus Extrudieren eines schlauchförmigen geschäumten Produkts, das Strecken des geschäumten Produkts, das Altern des gestreckten Schaums an Luft während mindestens 24 Stunden, um der Luft genügend Zeit zu geben durch die Zellenwände des Schaumes zu permeieren, um darin eine Druckerhöhung zu bewirken, und das Erwärmen des gealterten Schaums, um eine Nachexpansion zu bewirken, umfaßt.

4. Verfahren gemäß Anspruch 3, wobei das geschäumte Produkt nach dem Extrusionsschritt um das 1,2- bis 5-fache seines ursprünglichen Durchmessers gestreckt wird.

5. Verfahren gemäß Anspruch 3 oder 4, wobei das Styrolharz und das Treibmittel im Extruder einer Temperatur und einem Druck ausgesetzt werden, so daß das Harz nicht schäumt und die Viskosität des geschmolzenen Harzes abnimmt, wobei danach die Temperatur verringert wird, um die Viskosität des geschmolzenen Harzes zu erhöhen, und das geschmolzene Harz in eine Zone extrudiert wird, bei einer Temperatur und einem Druck, welche ausreichen, um ein Schäumen zu gestatten.

6. Verfahren gemäß Anspruch 5, wobei die Temperatur und der Druck, bei denen die Mischung nicht schäumt, von ungefähr 116°C (240°F) bis ungefähr 227°C (440°F) reicht, bei einem Druck von oberhalb ungefähr 4136 kPa (600 psig).

7. Verfahren gemäß einem der Ansprüche 3 bis 6, welches durchgeführt wird unter im wesentlichen Abwesenheit von Wasser.

8. Verfahren gemäß einem der Ansprüche 3 bis 7, welches ferner den Schritt des Zugebens eines Nukleierungsmittels zu dem Polystyrolharz umfaßt.

9. Verfahren gemäß Anspruch 8, wobei das Nukleirungsmittel Talk, Natriumbicarbonat/Zitronensäure, gasförmiges CO₂ oder Calciumsilikat ist.

Revendications

1. Mousse extrudée de polymère à cellules fermées dans laquelle les cellules ne contiennent pas d'agent moussant fluorocarboné, ladite mousse ayant été préparée à partir d'une composition moussante comprenant une résine de styrène et jusqu'à 20% en poids, par rapport au poids total de la composition, de 1,1-difluoroéthane, ladite mousse ayant une épaisseur de 1 à 5,08 mm (0,04 à 0,2 pouce), la mousse ayant été étirée après l'extrusion, vieillie à l'air durant une période d'au moins 24 heures et soumise à un chauffage pour provoquer la post-expansion de la mousse et le remplacement du 1,1-difluoroéthane par de l'air.

2. Mousse de polymère suivant la revendication 1, dans laquelle la mousse est étirée après l'extrusion en une quantité de 1,2 à 5 fois son diamètre original.

3. Procédé de production d'une mousse polymère à cellules fermées suivant la revendication 1, dont les cellules sont complètement remplies d'air, ledit procédé comprenant l'introduction de 1,1-difluoroéthane comme agent gonflant dans une résine styrénique fondue dans une extrudeuse, l'extrusion dans celle-ci d'un produit expansé tubulaire, l'étirement du produit moussant, le vieillissement de la mousse étirée à l'air durant au moins 24 heures pour laisser suffisamment de temps à l'air pour diffuser au travers des parois cellulaires de la mousse pour y provoquer une élévation de pression, et le chauffage de la mousse vieillie pour provoquer une post-expansion.

4. Procédé suivant la revendication 3, dans lequel le produit moussant est étiré en une quantité de 1,2 à 5 fois son diamètre original après l'étape d'extrusion.

5. Procédé suivant la revendication 3 ou 4, dans lequel ladite résine styrénique et l'agent gonflant sont soumis à une température et une pression dans l'extrudeuse telles que la résine ne mousse pas et que la viscosité de la résine en fusion diminue, après quoi la température est réduite pour augmenter la viscosité de la résine en fusion et la résine en fusion est extrudée dans une zone à une température et sous une pression suffisantes pour permettre la formation de mousse.

6. Procédé suivant la revendication 5, dans lequel la température et la pression auxquelles le mélange ne mousse pas sont d'environ 116°C (240°F) à environ 227°C (440°F), et une pression supérieure à environ 4136 kPa (600 psig).

7. Procédé suivant l'une quelconque des revendications 3 à 6, qui est réalisé en l'absence quasi totale d'eau.

8. Procédé suivant l'une quelconque des revendications 3 à 7, comprenant de plus l'étape d'addition d'un agent de nucléation à la résine de polystyrène.

9. Procédé suivant la revendication 8, dans lequel l'agent de nucléation est le talc, le bicarbonate de sodium/acide citrique, le CO₂ gazeux ou le silicate de calcium.

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